# US 4,396,496 A · Cracking process > Agents: this data is available as JSON from the patentgrep API and MCP server — see https://patentgrep.com/llms.txt - Number: US 4,396,496 A - Document ID: US4396496A - Status: Granted - Kind: A - Application number: 06/285,641 - Filed: 1981-07-21 - Granted: 1983-08-02 - Earliest claimed: 1981-07-21 - Assignees: Phillips Petroleum Company - Inventors: David R. Scharf; Earl H. Gray - Web page: https://patentgrep.com/patent/US4396496A ## CPC - C10G 11/05: Crystalline alumino-silicates, e.g. molecular sieves - C10G 11/187: {Controlling or regulating} - C10G 2300/705: Passivation - Y10S 208/01: Automatic control - C10G: CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION (cracking to hydrogen or synthesis gas C01B; cracking or pyrolysis of hydrocarbon gases to individual hydrocarbons or mixtures thereof of definite or specified constitution C07C; cracking to cokes C10B); RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES - Y10S: TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS ## Abstract Antimony compounds are employed to reduce catalyst attrition and improve catalyst performance in catalytic cracking units, especially in conjunction with strontium compounds. ## Claims ### Claim 1 In a process comprising (a) cycling a cracking catalyst in a catalytic cracking unit comprising a cracking zone and a regeneration zone, said cracking catalyst having a particle size principally within the range of from about 500 to about 10,000 microns; and (b) contacting the cracking catalyst with a hydrocarbon feed in the cracking zone to produce a cracked product and a coked cracking catalyst and with an oxygen-containing gas in the regeneration zone to produce a regenerated cracking catalyst which is cycled back to the cracking zone and a gaseous effluent stream also containing a concentration of catalyst fines having a particle size principally below about 100 microns; the improvement comprising (c) adding an antimony compound to the catalytic cracking unit; and (d) adjusting the addition of said antimony compound so as to maintain the concentration of catalyst fines below a predetermined value. ### Claim 2 (depends on 1) A process as in claim 1 further comprising (a) establishing a first signal representative of the concentration of catalyst fines in the gaseous effluent stream from the regeneration zone; and (b) adjusting the addition of antimony compound in response to said first signal. ### Claim 3 (depends on 2) A process as in claim 2 further comprising (a) establishing a second signal representative of a desired maximum concentration of catalyst fines in the gaseous effluent stream from the regeneration zone; (b) comparing the first signal to the second signal and establishing a third signal in response to said comparison; and (c) adjusting the addition rate of the antimony compound in response to the third signal. ### Claim 4 (depends on 3) A process as in claim 3 wherein from about 0.005 to about 0.5 weight percent antimony, based on weight elemental antimony to total weight of cracking catalyst is maintained on the cracking catalyst, and wherein the antimony compound is selected from the group consisting of antimony oxide, antimony alkyl oxide, antimony aryl oxide, antimony sulfate, antimony sulfide, and antimony hydrocarbyl thiophosphate. ### Claim 5 (depends on 4) A process as in claim 4 wherein the antimony compound comprises antimony di-n-propylphosphorodithioate which is added to the cracking unit in combination with the hydrocarbon feed. ### Claim 6 A process comprising (a) circulating an inventory of cracking catalyst in a catalytic cracking unit comprising a cracking zone and a regeneration zone: (b) contacting the cracking catalyst with a hydrocarbon feedstock in the cracking zone to produce a coked cracking catalyst and a cracked product which contains methane and molecular hydrogen and with an oxygen-containing gas in the regeneration zone to produce a regenerated cracking catalyst which is introduced back to the cracking zone and a gaseous effluent stream also containing a concentration of catalyst fines at least a portion of which have a particle size below about 100 microns; (c) circulating together with the cracking catalyst a strontium compound in an amount of from about 0.01 to about 1 weight percent, based on the elemental weight of strontium and the total weight of the catalyst inventory, including the strontium compound; and (d) circulating together with the cracking catalyst an antimony compound in an amount of from about 0.005 to about 0.5 weight percent, based on the elemental weight of antimony and the total weight of the catalyst inventory, including antimony. ### Claim 7 (depends on 6) A process as in claim 6 wherein from about 0.1 to about 1 weight percent of strontium and from about 0.01 to about 0.5 weight percent of antimony are circulated together with the catalyst inventory, and a major portion of said cracking catalyst was a particle size within the range of from about 500 to about 10,000 microns. ### Claim 8 (depends on 6) A process as in claim 6 wherein the catalyst inventory comprises zeolite-modified silica-alumina cracking catalyst, a major portion of which has a particle size within the range of from about 3000 to about 6000 microns. ### Claim 9 (depends on 7) A process as in claim 7 wherein a sufficient amount of strontium is circulated with the catalyst inventory to lower the ratio between the molecular hydrogen and methane in the cracked product from the cracking zone and wherein a sufficient amount of antimony is circulated with the catalyst inventory to lower the concentration of catalyst fines in the effluent stream from the regeneration zone. ### Claim 10 (depends on 8) A process as in claim 8 further comprising introducing into the cracking unit a strontium compound selected from the group consisting of strontium oxide, strontium alkyl oxide, strontium aryl oxide and strontium sulfate and an antimony compound selected from the group consisting of antimony oxide, antimony alkyl oxide, antimony aryl oxide, antimony sulfate, antimony sulfide and antimony hydrocarbyl thiophosphate. ### Claim 11 (depends on 8) A process as in claim 8 wherein the strontium compound comprises strontium sulfate and the antimony compound comprises antimony O,O-di-n-propylphosphorodithioate. ### Claim 12 (depends on 11) A process as in claim 11 wherein the strontium compound and the antimony compound are introduced into the cracking unit in combination with the hydrocarbon feedstock which is at a temperature of between about 50.degree. C. and about 160.degree. C., and wherein the hydrocarbon feedstock contains less than 10 parts per million of combined nickel, vanadium, copper, and iron, not including "tramp" iron, on an elemental basis based on total weight of feedstock. ### Claim 13 (depends on 6) A cracking catalyst composition formed in accordance with a process as set forth in claim 6.